CN206767965U - A kind of low pressure methanol synthesis system - Google Patents
A kind of low pressure methanol synthesis system Download PDFInfo
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- CN206767965U CN206767965U CN201720469825.7U CN201720469825U CN206767965U CN 206767965 U CN206767965 U CN 206767965U CN 201720469825 U CN201720469825 U CN 201720469825U CN 206767965 U CN206767965 U CN 206767965U
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Abstract
It the utility model is related to a kind of low pressure methanol synthesis system, first-stage reactor and second reactor employ boiler feedwater forced circulation and move thermal technology, move hot quickness and high efficiency, device arrangement can effectively be simplified, reduce the construction investment of device frame, and be not in because the arrangement altimeter of drum is not calculated accurately really, the problems such as causing circulating ratio decline, take thermal effect undesirable；Circulating ratio can effectively be improved by forced circulation, efficient and rational utilizes reaction heat, strengthens heat-transfer effect；Cross-line is provided between synthesic gas compressor outlet and second reactor entrance, realize stable operation of the two-stage reactor catalyst in the different phase of service life, also accommodating strong adjustment can be entered to the load of reactor by cross-line, and then the production ratio of middle pressure steam and low-pressure steam is adjusted flexibly；The on-position of fresh synthesis gas can reduce heat exchange area, the specification of synthesis gas thermosistor behind synthesis gas thermosistor, reduce construction investment.
Description
Technical field
It the utility model is related to a kind of low pressure methanol synthesis system.
Background technology
Methanol is a kind of important C1 Elementary Chemical Industry product and Organic Chemicals, and methanol-fueled CLC is a volume-diminished
Reversible exothermic reaction.Since nineteen twenty-three, BASF Aktiengesellschaft successfully developed HTHP gas-phase methanol synthesis technique,
Methanol synthesizing process experienced synthesis atmospheric pressure by high pressure to low pressure, synthesis temperature by high temperature to low temperature, reactor by thermal insulation to
The technology development course of isothermal.In recent years, energy consumption, environmental requirement are persistently carried with the progress and country of methanol synthesis technology
Height, methanol synthesis technology continue to develop to maximization, energy-saving, environment-friendly type direction.
The Chinese invention patent application of Application No. 201510658690.4 discloses《A kind of different brackets steam of producing
Energy-saving ultra-large methane synthesizing method and device》, following technological deficiency be present in the technique：
(1) first methanol reactor and the second methanol reactor remove reaction heat and employ Natural Circulation technology, the skill
The drum arrangement requirement that art pair is connected with reactor is harsh, heat exchange efficiency Low investment height be present, is unfavorable for reactor maximization etc.
Problem；
(2) effective reaction Load Regulation means are lacked between first reactor and second reactor, this can produce two
Negative consequence：One is when first reactor and second reactor catalyst are in different service life states, can not be to string
The two-stage reactor load of connection realizes effectively regulation；The second is can not centering pressure drum and the appropriate tune of low-pressure drum gas production progress
Section；
(3) on-position of fresh synthesis gas and circulating air is not reasonable, due to pressure ratio of the fresh synthesis gas through compressor
Larger, the temperature after compression is higher, is now mixed with the circulating air of low temperature, causes mixture temperature to raise, then entered again
Row heat exchange can make logarithmic mean temperature difference (LMTD) diminish, and then increase heat exchange area, heat exchanger specification and construction investment.
Therefore, for the synthesis system of current methanol, improved up for further.
Utility model content
Technical problem to be solved in the utility model is the present situation for prior art, there is provided it is quick high that one kind moves heat
Effect, reactor load low pressure methanol synthesis system strong, utilization of Heat of Reaction is efficient and rational easy to adjust, the system can be significantly simple
Makeup puts arrangement, effectively reduces construction investment and energy consumption.
Technical scheme is used by the utility model solves above-mentioned technical problem：A kind of low pressure methanol synthesis system, its
It is characterised by including：
Synthesic gas compressor, there is gas outlet and the air inlet being connected with fresh synthesis gas；
Gas-gas heat exchanger, it is connected with the synthesic gas compressor and can receives the synthesis after synthesic gas compressor pressurizes
Gas；
First-stage reactor, for two and it is connected in parallel, is connected with the gas-gas heat exchanger and can receive through gas-gas heat exchange
Synthesis gas after device preheating, the port of export of the first-stage reactor are provided with and reacted high temperature first order reaction gas can be transferred back into gas
The pipeline of gas heat exchanger；
Second reactor, the high temperature one-level cooled down through gas-gas heat exchanger that is connected with the gas-gas heat exchanger and can receive are anti-
Should gas；
Thermosistor is synthesized, be connected and can receive the two level exported in second reactor after reaction with the second reactor
Reaction gas, the synthesis thermosistor has can be using part second order reaction gas as circulating air and the synthesis gas of synthesic gas compressor output
The first outlet mixed；The synthesis thermosistor uses deflection bar type heat exchange structure, to improve heat exchange efficiency；
Aerial cooler, it is connected and can receives through synthesizing thermosistor cooling with the second outlet of the synthesis thermosistor
Second order reaction gas；
Water cooler, the outlet with the aerial cooler are connected；
Separator, the outlet with the water cooler are connected and to carry out gas-liquid separation, have the liquid that will can be isolated
The first outlet mutually exported and the second outlet that the small part circulating air isolated can be discharged as periodic off-gases；
Recycle gas compressor, import are connected with the separator and can receive the gas phase that separator is isolated, outlet with
The import of synthesis thermosistor is connected；
Low-pressure drum, there is the import for the low-pressure boiler water input from battery limit (BL)；
Low pressure recycle pump, import are connected with the outlet of low-pressure drum and can receive boiler feedwater in low-pressure drum and added
Pressure, the outlet of the low pressure recycle pump is connected with second reactor；It is also associated between the second reactor and low-pressure drum
The feedwater of the low-pressure boiler after absorption heat can be made to be back to the pipeline of low-pressure drum progress gas-liquid separation from second reactor；
Synthesic gas compressor turbine, it is connected with the low-pressure drum and the low pressure saturation from low-pressure drum can be received and steam
Vapour, the synthesic gas compressor turbine have exhaust steam outlet；
Middle pressure drum, there is the import for the medium-pressure boiler feedwater input from battery limit (BL)；
Medium pressure cycle pump, import press boiler feedwater in drum to be added in being connected and can receive with the outlet of middle pressure drum
Pressure, the outlet of the Medium pressure cycle pump is connected with first-stage reactor；It is also associated between the first-stage reactor and middle pressure drum
Medium-pressure boiler feedwater after absorption heat can be back to the pipeline of middle pressure drum progress gas-liquid separation from first-stage reactor；And
Superheater, it is connected with medium pressure drum so as to pressure drum is isolated in receiving middle pressure saturated vapor and carries out
Heating, the superheater have and saturated vapor can will be pressed to be delivered to the first outlet of synthesic gas compressor turbine and by affluence in part
In press through the second outlet that vapours is exported.
Synthesis gas can be compressed from synthesis gas preferably, being provided between the synthesic gas compressor and second reactor
Machine directly transports to the cross-line of second reactor.Using such structure, in order to the activity according to catalyst in first-stage reactor
Degree, the sharing of load of two-stage reactor is adjusted by the fresh synthesis gas amount adjusted into second reactor.
Compared with prior art, the utility model has the advantage of：
First-stage reactor and second reactor of the present utility model employ boiler feedwater forced circulation and move thermal technology, no
Hot quickness and high efficiency is only moved, the setting height(from bottom) and technical requirements of drum and low-pressure drum are pressed in can also effectively reducing, is greatly simplified
Device arrangement, while the construction investment of device frame is also reduced, and be not in because the arrangement of drum highly calculates not
Accurately, the problems such as causing circulating ratio decline, take thermal effect undesirable；By forced circulation, circulation can also be effectively improved
Multiplying power, efficient and rational utilizes reaction heat, strengthens heat-transfer effect, so as to reduce reactor specification；
The utility model exports in synthesic gas compressor and cross-line is provided between second reactor entrance, in actual motion
By adjusting the reaction sharing of load of two-stage reactor, so as to realize different phase of the two-stage reactor catalyst in service life
Stable operation, while in normal operation, can also enter accommodating strong adjustment to the load of reactor by cross-line, and then
The production ratio of middle pressure steam and low-pressure steam can be adjusted flexibly；
The on-position of fresh synthesis gas can reduce synthesis controlled atmosphere behind synthesis gas thermosistor in the utility model
The heat exchange area of warm device, specification, reduce construction investment.
Brief description of the drawings
Fig. 1 is the structural representation of the utility model embodiment.
Embodiment
The utility model is described in further detail below in conjunction with accompanying drawing embodiment.
As shown in figure 1, the low pressure methanol synthesis system of the present embodiment includes synthesic gas compressor 2, gas-gas heat exchanger 4, one
Stage reactor, second reactor 7, synthesis thermosistor 8, aerial cooler 9, water cooler 10, separator 11, recycle gas compressor 3,
Low-pressure drum 15, low pressure recycle pump 16, synthesic gas compressor turbine 1, middle pressure drum 12, Medium pressure cycle pump 13 and superheater 14.
Wherein, synthesic gas compressor 2 has gas outlet and the air inlet being connected with fresh synthesis gas.Gas-gas heat exchanger 4
The synthesis gas after the pressurization of synthesic gas compressor 2 can simultaneously be received by being connected with synthesic gas compressor 2.First-stage reactor 5,6 is two
Individual and be connected in parallel, first-stage reactor 5,6 is connected with gas-gas heat exchanger 4 and can receive the conjunction after gas-gas heat exchanger 4 preheats
Into gas, the port of export of first-stage reactor 5,6 is provided with and reacted high temperature first order reaction gas can be transferred back into gas-gas heat exchanger 4
Pipeline.Second reactor 7 is connected with gas-gas heat exchanger 4 can simultaneously receive the high temperature first order reaction gas cooled down through gas-gas heat exchanger 4.
Synthesis thermosistor uses deflection bar type heat exchange structure, and the synthesis thermosistor 8 is connected with second reactor 7 and to receive two level anti-
The second order reaction gas exported after being reacted in device 7 is answered, synthesis thermosistor 8 has can be using part second order reaction gas as circulating air and conjunction
The first outlet that the synthesis gas exported into air compressor 2 is mixed.The second outlet of aerial cooler 9 and synthesis thermosistor 8
Be connected and can receive the second order reaction gas cooled down through synthesizing thermosistor 8.Water cooler 10 is connected with the outlet of aerial cooler 9
Connect.Separator 11 is connected with the outlet of water cooler 10 and to carry out gas-liquid separation, and the liquid phase isolated can be carried out by having
The first outlet of output and the second outlet that the small part circulating air isolated can be discharged as periodic off-gases.Recycle gas compressor
3 import is connected with separator 11 and can receive the gas phase that separator 11 is isolated, and exports the import phase with synthesizing thermosistor 8
Connection.Low-pressure drum 15 has the import for the low-pressure boiler water input from battery limit (BL).The import of low pressure recycle pump 16 and low pressure
The outlet of drum 15, which is connected and can receive boiler feedwater in low-pressure drum 15, is pressurizeed, the outlet of the low pressure recycle pump 16 with
Second reactor 7 is connected；Between the second reactor 7 and low-pressure drum 15 it is also associated with that the low pressure after absorption heat can be made
Boiler feedwater is back to the pipeline of the progress gas-liquid separation of low-pressure drum 15 from second reactor 7.Synthesic gas compressor turbine 1 with it is low
Pressure drum 15 is connected and can receive the low-pressure saturated steam from low-pressure drum 15, and the synthesic gas compressor turbine 1 has weary
Vapor outlet.Middle pressure drum 12 has the import for the medium-pressure boiler feedwater input from battery limit (BL).The import of Medium pressure cycle pump 13 with
The outlet of middle pressure drum 12 presses boiler feedwater in drum 12 to be pressurizeed in being connected and receiving, and the Medium pressure cycle pump 13 goes out
Mouth is connected with first-stage reactor 5,6；It is also associated between first-stage reactor 5,6 and middle pressure drum 12 after absorbing heat
Medium-pressure boiler feedwater is back to the pipeline of middle pressure drum 12 progress gas-liquid separation from first-stage reactor 5,6.Superheater 14 and middle pressure
Drum 12 is connected so as to pressure drum 12 is isolated in receiving middle pressure saturated vapor and heated, and superheater 14 has can general
Pressed in part saturated vapor be delivered to synthesic gas compressor turbine 1 first outlet and will it is rich in press through vapours carry out it is defeated
The second outlet gone out.Being provided between synthesic gas compressor 2 and second reactor 7 can be straight from synthesic gas compressor 2 by synthesis gas
The cross-line a for transporting to second reactor 7 is met, in order to the level of activity according to catalyst in first-stage reactor, is entered by adjusting
The sharing of load of the fresh synthesis gas amount adjustment two-stage reactor of second reactor.
When being produced using the low pressure methanol synthesis system of the present embodiment, the fresh synthesis gas from upstream process is (main
It is H to want component2、CO、CO2, mol ratio：(H2-CO2)/(CO+CO2)=2.05~2.15) through synthesic gas compressor 2 it is forced into 6.0
~10.0MPaG, mixed with the circulating air preheated by synthesis gas thermosistor 8, then 210~250 are preheated to through gas-gas heat exchanger 4
DEG C, the first-stage reactor 5,6 in parallel into two, under catalyst for synthesizing copper based methanol effect, carry out methanol synthesis reaction；One
The high temperature first order reaction temperature degree that stage reactor 5,6 exports is 250~280 DEG C, and 200~220 are cooled to through gas-gas heat exchanger 4
DEG C, continue methanol synthesis reaction into second reactor 7；The second order reaction gas that second reactor 7 exports is through synthesizing temperature adjustment
Device 8 exchanges heat with circulating air, and second order reaction gas is cooled to 100~140 DEG C, and second order reaction gas passes through aerial cooler 9 successively again
60~80 DEG C are cooled to, 35~45 DEG C are cooled to by water cooler 10, separator 11 is finally entered and carries out gas-liquid separation, isolate
Gas phase enter as circulating air after recycle gas compressor 3 pressurizes and return to synthesis loop, while in order to prevent inert gas from accumulating,
The part circulating air isolated discharges as periodic off-gases, and the mol ratio of periodic off-gases and fresh synthesis gas is 3~5:100, isolate
Liquid phase crude carbinol output and fed downstream process continue with；
Low-pressure boiler water from battery limit (BL) enters low-pressure drum 15, and boiler feedwater is through low pressure recycle pump in low-pressure drum 15
Enter second reactor 7 after 16 pressurizations, remove liberated heat during second reactor 7 reacts, absorb the low-pressure boiler after heat
Feedwater returns to low-pressure drum 15 and carries out vapour-liquid phase separation, 1.0~2.0MPaG of output low-pressure saturated steam, low-pressure saturated steam
Into synthesic gas compressor turbine 1, used as driving steam；
Medium-pressure boiler feedwater from battery limit (BL) presses drum 12 in entering, and boiler feedwater is through Medium pressure cycle in middle pressure drum 12
Pump 13 enters first-stage reactor 5,6 after pressurizeing, liberated heat during first-stage reactor 5,6 reacts is removed, in absorbing after heat
Press boiler feedwater to press drum 12 to carry out vapour-liquid phase separation in returning, saturated vapor, middle pressure saturation are pressed in 2.5~4.0MPaG of output
Steam is superheated to 360~400 DEG C through superheater 14, partly send synthesic gas compressor turbine 1, uses, supplements as driving steam
The insufficient section of low-pressure steam, in press through the rich part of vapours and enter corresponding steam pipe system.
In the present embodiment, set and fresh synthesis gas can be synthesized certainly between synthesic gas compressor 2 and second reactor 7
Air compressor directly transports to the cross-line a of second reactor, in order to the level of activity according to catalyst in first-stage reactor, passes through
Sharing of load of the regulation into the fresh synthesis gas amount adjustment two-stage reactor of second reactor；Certainly, can also be steamed according to full factory
The balance of vapour, the load of two-stage reactor is adjusted so as to adjust the production ratio of two kinds of grade steam.
Claims (2)
- A kind of 1. low pressure methanol synthesis system, it is characterised in that including：Synthesic gas compressor (2), there is gas outlet and the air inlet being connected with fresh synthesis gas；Gas-gas heat exchanger (4), it is connected with the synthesic gas compressor (2) and can receives after synthesic gas compressor (2) pressurization Synthesis gas；First-stage reactor (5,6), for two and it is connected in parallel, is connected with the gas-gas heat exchanger (4) and can receive through gas gas Synthesis gas after heat exchanger (4) preheating, the port of export of the first-stage reactor (5,6) is provided with can be anti-by reacted high temperature one-level Should gas be transferred back to the pipelines of gas-gas heat exchanger (4)；Second reactor (7), be connected and can receive the high temperature cooled down through gas-gas heat exchanger (4) with the gas-gas heat exchanger (4) First order reaction gas；Thermosistor (8) is synthesized, being connected with the second reactor (7) and receiving in second reactor (7) exports after reaction Second order reaction gas, the synthesis thermosistor (8) have can be using part second order reaction gas as circulating air and synthesic gas compressor (2) The first outlet that the synthesis gas of output is mixed；Aerial cooler (9), it is connected and can receives through synthesizing thermosistor (8) with the second outlet of the synthesis thermosistor (8) The second order reaction gas of cooling；Water cooler (10), the outlet with the aerial cooler (9) are connected；Separator (11), the outlet with the water cooler (10) are connected and to carry out gas-liquid separation, and having will isolate The liquid phase first outlet exported and the second outlet that the small part circulating air isolated can be discharged as periodic off-gases；Recycle gas compressor (3), import are connected with the separator (11) and can receive the gas phase that separator (11) is isolated, Export and be connected with the import of synthesis thermosistor (8)；Low-pressure drum (15), there is the import for the low-pressure boiler water input from battery limit (BL)；Low pressure recycle pump (16), import be connected with the outlet of low-pressure drum (15) and can receive low-pressure drum (15) interior boiler to Water is pressurizeed, and the outlet of the low pressure recycle pump (16) is connected with second reactor (7)；The second reactor (7) with it is low It is also associated with that the low-pressure boiler feedwater after absorption heat can be made to be back to low-pressure steam from second reactor (7) between pressure drum (15) Wrap the pipeline that (15) carry out gas-liquid separation；Synthesic gas compressor turbine (1), it is connected with the low-pressure drum (15) and can receives low from low-pressure drum (15) Saturated vapor is pressed, the synthesic gas compressor turbine (1) exports with exhaust steam；Middle pressure drum (12), there is the import for the medium-pressure boiler feedwater input from battery limit (BL)；Medium pressure cycle pump (13), import be connected with the outlet of middle pressure drum (12) and in receiving pressure drum (12) interior boiler to Water is pressurizeed, and the outlet of the Medium pressure cycle pump (13) is connected with first-stage reactor (5,6)；The first-stage reactor (5,6) It is also associated with the medium-pressure boiler after absorption heat being fed water from first-stage reactor (5,6) between middle pressure drum (12) and is back to Middle pressure drum (12) carries out the pipeline of gas-liquid separation；AndSuperheater (14), it is connected with medium pressure drum (12) so as to which the middle pressure saturation for pressing in receiving drum (12) to isolate is steamed Vapour is simultaneously heated, and the superheater (14) has and in part saturated vapor can will be pressed to be delivered to synthesic gas compressor turbine (1) First outlet and will it is rich in press through the second outlet that vapours is exported.
- 2. low pressure methanol synthesis system according to claim 1, it is characterised in that：The synthesic gas compressor (2) and two Being provided between stage reactor (7) can directly transport to synthesis gas from synthesic gas compressor (2) cross-line of second reactor (7) (a)。
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| CN201720469825.7U CN206767965U (en) | 2017-04-28 | 2017-04-28 | A kind of low pressure methanol synthesis system |
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| CN201720469825.7U CN206767965U (en) | 2017-04-28 | 2017-04-28 | A kind of low pressure methanol synthesis system |
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